• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    An improved process for removing sulfur oxides from gas mixtures with a solid acceptor for sulfur oxides wherein the solid acceptor is regenerated with a steam-diluted reducing gas and the regeneration off-gas is fed to a Claus sulfur recovery process. The improvement comprises cooling the regeneration off-gas to condense the water vapor contained therein, contacting the cooled off-gas with a sulfur dioxide-selective liquid absorbent, passing the fat liquid absorbent to a buffer zone and then to a stripping zone wherein the absorbed SO2 is recovered from the liquid absorbent and is supplied to the sulfur recovery process. By operating in this manner, fluctuations in the sulfur dioxide concentration of the regeneration off-gas are leveled-out and on relatively concentrated sulfur dioxide stream is supplied to the sulfur recovery process at a substantially constant rate.
    公开号:SU778702A3
    申请号:SU721750263
    申请日:1972-02-17
    公开日:1980-11-07
    发明作者:Грюндал Виллем；Макс Ленц Вальтер
    申请人:Шелл Интэрнэшнл Рисерч Маатсхаппий (Фирма)；
    IPC主号:
    专利说明:

    Scuffed with a liquid absorbent, after sizing from a saturated absorbent, sulfuric anhydride is desorbed after 10–80 minutes from a saturated absorbent in the buffer zone. Desorption of sulfurous anhydride from a liquid absorbent can be carried out and heated. It is advisable to use N-methylpyrrolidine, xylidine, dimethylanil, and sulfinol as liquid absorbents. High selectivity to sulfur dioxide is combined in these compounds with a high absorption capacity.
    The process according to the invention can be carried out so that the liquid saturated absorbent is heated when passing through the buffer zone, and the duration of the absorbent in the buffer zone should be at least 10 minutes.
    As a result of optimal selection of the size of the buffer zone and control of the fluid flow from the buffer zone to the heating zone, it is possible to compensate for fluctuations in the concentration of sulfur dioxide in the regeneration gas obtained during the regeneration of solid sorbents, and to ensure an almost constant concentration of SOa fed to the Claus plant.
    The buffer zone can be structurally designed either as a separate vessel or as part of an apparatus in which the absorption of SO2 is carried out by a liquid absorbent. The absorption is carried out at 10-60 ° C and a pressure of 1-10 atm.
    The residence time in the buffer zone is determined depending on the duration of the fluctuations in the concentration of sulfur dioxide in the regeneration gas. The optimal time is to stay in the buffer zone for 24-80 minutes. Example 1. The plant is supplied with waste flue gases containing sulfuric anhydride in an amount equivalent to 10.9 g of sulfur per day.
    The composition of the flue gases after their purification on solid sorbents remains an amount of sulfurous anhydride, equivalent to 1.1 tons of sulfur per day. These gases are released into the atmosphere. An amount of S02, equivalent to 9.8 tons of sulfur per day, is supplied to the absorption by the liquid absorbent. In the composition of gases after absorption, an amount of SO2, equivalent to 0.1 g of sulfur per day, is removed. An amount of sulfuric anhydride equivalent to 9.7 tons per day is supplied to Claus Plant, and hydrogen sulfide is sent to the installation of Claus in an amount equivalent to 19.4 tons per day. 28.3 tons of elemental sulfur are shipped from the Klaus plant per day. The gases after the installation of Claus, as well as the gases from the stage of absorption of S02 by a liquid absorbent, are directed to the afterburner. Gaseous products after furnaces and doji {ayi, containing SO2 in an amount corresponding to 0.9 g per day, are displaced with a total volume of gases and supplied to purification with solid sorbents.
    The overall degree of desulfurization reaches 96.3%.
    Example 2. Exhaust flue gases, holding at 0.15 vol. % S02, are shifted with gaseous products after the afterburning furnace, as in Example 1, in a ratio of about 90: 1. The concentration of SO2 in the gases after the afterburner is 1.24 vol. %
    The resulting gas mixture at 500 ° C is sent to a reactor loaded with an absorber, representing alumina with copper deposited on it. The gases after the reactor contain 0.015% S02 and have a temperature of 420 ° C. After saturation, the absorber is regenerated by passing a reducing gas diluted under a pressure of 1.5 atm at 360 ° C. The result is a regeneration gas containing 5.67% SO2 and having a temperature of 425 ° C. The regeneration gas is cooled and passed through a separator. In the separator, the gas is separated from the condensate and discharged into the amount of 344 under a pressure of 1.4 atm and temperature. The concentration of sulfurous anhydride is 66 vol. % The gas is then sent to an absorber irrigated with water at 40 ° C. From the absorber, the aqueous solution is fed to a stripping column. The residence time of the solution in the absorber is 36 minutes, after which the solution is fed to a stripping column, resulting in a steam-saturated stream of gaseous sulfuric anhydride containing 90.3% SO2, which is fed to the sulfur plant. Acid gas containing 93% of hydrogen sulfide is fed to the same plant.
    The post-installation gases, containing 2% H2S and 1% SO2, are directed to the afterburner, where the gases after the absorber and the required amount of air are also directed.
    The degree of flue gas purification is 90%.
    权利要求:
    Claims (2)
    [1]
    Invention Formula
    The method of purification of gases from sulfur dioxide, which includes its absorption on a solid sorbent, followed by regeneration of the latter with the production of a regenerating gas containing sulfur dioxide, which is processed to elemental sulfur according to the Claus method, in order to ensure a constant concentration of sulfur dioxide. anhydride supplied for processing according to the Claus method, the sulfuric anhydride from the regeneration gas is absorbed by the liquid absorbent, and then from the saturated absorbent after Extracts it in the buffer zone for 10-80 min. sulfur dioxide is desorbed. 1. The patent of Germany No. 22.11.56. 5b Sources of information taken into account at the examination 952892, cl. 12 17/60,
    [2]
    2. US patent No. 3702884, cl. 423-222, 778702 14.11.72 (prototype).
    类似技术:
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    US4267162A|1981-05-12|Process and apparatus for the exploitation of the sulfur compounds contained in gases containing oxygen and a high water vapor content
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    同族专利:
    公开号 | 公开日
    NL169415B|1982-02-16|
    AT319274B|1974-12-10|
    AU466494B2|1975-10-30|
    SE380507B|1975-11-10|
    DD95364A5|1973-02-05|
    BE779165A|1972-08-10|
    NO133705B|1976-03-08|
    FR2127024B1|1974-08-30|
    ES399876A1|1974-11-16|
    FR2127024A1|1972-10-13|
    AU3911672A|1973-08-23|
    GB1363164A|1974-08-14|
    JPS5631281B1|1981-07-20|
    CH593208A5|1977-11-30|
    NL7102211A|1972-08-22|
    ZA721048B|1972-10-25|
    CA979184A|1975-12-09|
    NO133705C|1976-06-16|
    DE2207515A1|1972-08-31|
    IT947666B|1973-05-30|
    NL169415C|1983-01-17|
    CS155109B2|1974-05-30|
    US3764665A|1973-10-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2747968A|1951-05-07|1956-05-29|Pigache Pierre Gustave Adolphe|Dry process for the recovery of sulfur from gases|
    US3645671A|1969-10-24|1972-02-29|Exxon Research Engineering Co|Flue gas desulfurization with ammonium sulfite|
    NL7007611A|1970-05-27|1971-11-30|US3928547A|1972-06-30|1975-12-23|Allied Chem|Process for the reduction of sulfur dioxide|
    US4036943A|1972-09-15|1977-07-19|Institut Francais Du Petrole|Process for removing sulfur dioxide from a gas and producing sulfur therefrom|
    NL170663B|1972-09-28|1982-07-01|Shell Int Research|PROCESS FOR DE-SULFURING GASES CONTAINING SULFUR DIOXIDE USING A FIXED SULFUR DIOXIDE ACCEPTOR.|
    US3920421A|1974-01-15|1975-11-18|Chemsoil Corp|Removal of oxides of nitrogen from gas streams which also contain sulfur dioxide|
    US3895101A|1974-06-07|1975-07-15|Nittetsu Kakoki Kk|Method for the treatment of waste gas from claus process|
    US3985861A|1974-09-16|1976-10-12|Shell Oil Company|Process for removing sulfur compounds from claus off-gases|
    US3970744A|1974-11-07|1976-07-20|Ralph M. Parsons Company|Process for the production of sulfur from sulfur dioxide extracted from gas streams|
    DE2531930A1|1975-07-17|1977-01-20|Metallgesellschaft Ag|PROCESS FOR THE RECOVERY OF ELEMENTARY SULFUR FROM GASES RICH IN CARBON DIOXIDE, SULFUR COMPOUNDS AND POLLUTIONS|
    US4041131A|1975-10-14|1977-08-09|Uop Inc.|Sulfur recovery process|
    US4041142A|1975-12-08|1977-08-09|Battelle Memorial Institute|Method for removing sulfur oxide from waste gases and recovering elemental sulfur|
    US4124685A|1976-06-08|1978-11-07|Tarhan Mehmet O|Method for substantially complete removal of hydrogen sulfide from sulfur bearing industrial gases|
    US4110087A|1976-11-02|1978-08-29|Uop Inc.|Sulfur dioxide removal by absorption and fractionation|
    US4233276A|1979-03-30|1980-11-11|Standard Oil Company |Process for the desulfurization of waste gases|
    JPS6341845B2|1979-09-07|1988-08-19|Hitachi Ltd|
    US4477426A|1983-04-29|1984-10-16|Foster Wheeler Energy Corporation|Process for preparing a sulfur dioxide containing gas stream for reaction with coal|
    DE3340631A1|1983-11-10|1985-05-23|Linde Ag, 6200 Wiesbaden|METHOD FOR SEPARATING GAS AND / OR LIQUID MIXTURES|
    US4636371A|1985-09-09|1987-01-13|Phillips Petroleum Company|Removal of sulfur oxides from fluid streams|
    US5798088A|1993-03-30|1998-08-25|Research Triangle Institute|Method for producing elemental sulfur from sulfur-containing gases|
    US5591417A|1992-04-15|1997-01-07|Mobil Oil Corporation|Removing SOx, CO and NOx from flue gases|
    DE69331577T2|1992-04-15|2002-10-31|Exxonmobil Oil Corp|METHOD AND APPLICATION OF A DEVICE FOR THE EXTRACTION OF SULFUR FROM GAS FLOWS CONTAINING SULFUR HYDROCHLORIC ACID|
    US5458861A|1992-04-15|1995-10-17|Mobil Oil Corporation|Desulfurizing a gas stream|
    US5229091A|1992-04-15|1993-07-20|Mobil Oil Corporation|Process for desulfurizing Claus tail-gas|
    US5547648A|1992-04-15|1996-08-20|Mobil Oil Corporation|Removing SOx, NOX and CO from flue gases|
    US5514351A|1992-04-15|1996-05-07|Mobil Oil Corporation|Desulfurizing tailgas from sulfur recovery unit|
    US5292492A|1992-05-04|1994-03-08|Mobil Oil Corporation|Recovering sulfur from ammonia acid gas stream|
    GB2267904A|1992-06-19|1993-12-22|Exxon Research Engineering Co|Method of recovering and/or obtaining a sulphur moiety|
    US5494879A|1993-02-26|1996-02-27|Regents, University Of California|Catalyst for the reduction of sulfur dioxide to elemental sulfur|
    FR2809638B1|2000-06-02|2002-12-06|Inst Francais Du Petrole|PROCESS AND DEVICE FOR REGENERATING SPENT ABSORBENTS FROM THE TREATMENT OF THERMAL GENERATOR FUMES|
    US7033565B2|2003-08-16|2006-04-25|Haldor Topsoe A/S|Production of sulphuric acid from a feed gas with varying concentration of sulphur dioxide|
    US7311891B2|2005-03-09|2007-12-25|Basf Catalysts Llc|Process for the recovery of sulfur from Claus tail gas streams|
    CN102120122A|2010-12-14|2011-07-13|东营方圆有色金属有限公司|Selenium absorption column dilute acid concentrating process|
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    CN103539076A|2013-09-30|2014-01-29|东华工程科技股份有限公司|Claus sulfur recycling device|
    RU2754859C2|2017-03-08|2021-09-08|Шелл Интернэшнл Рисерч Маатсхаппий Б.В.|Method for removing so2 from gas with temporarily high so2 content|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NLAANVRAGE7102211,A|NL169415C|1971-02-19|1971-02-19|METHOD FOR CONVERTING IN ELEMENTAL SULFUR OF SULFUR OXIDES, GASES CONTAINING SULFUR OXIDES|
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